System for the conversion of heat



Jan. 14, 1936. v. NESSELMANN ET AL 1 SYSTEM FOR THE CONVERSION OF HEAT Filed Dec. 16, 1935 6 Sheefs-Sheet l AT M/Vasselma m I Jan. 14, 1936. K. V. N E$SELMANN ETAL. I 2,027,610 SYSTEM FOR THE CONVERSION OFIHEAT Filed Dec. 16, 1935; a Sheets-Sheet 2 jig/Z Ig /w Jan. 14, 1936. K. v. NESSELMANN ET AL 2,027,610

SYSTEM FOR THE CQNVERSION OF HEAT Filed Dec. 16, 1955 6 Sheets-Sheet 3 Jan. 14, 1936. K. v. NESSELMANN E! AL 2,027,610

SY STEM FOR THE CONVERSION OF HEAT 6 Sheets-Sheet 4 Filed Dec. 16, 1933 Jan. 14, 1936. K. v. NESSELMANN EITAL I 2,

SYSTEM FOR THE CONVERSION OF HEAT Filed Dec. 16, 1935 Sheets-Sheet 5 if? if! .30.?

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' .Ean. 14, 1936. K. v. NESSELMANN EI'AL 2,027,610

SYSTEM FOR THE CONVERSION. OF HEAT WTTOKNEYS .Patenteci Jan. 14, 1936 PATENT OFFICE 7 2,027,610 SYSTEM FOR THE CONVERSION OF HEAT Kurt V. Nessclmann, Berlin-Siemensstadt, and

Edmund Altcnkirch, Ncuenhagen,

Germany, assignors near Berlin,

to Sieme -Schuckcrtwerke Aktiengesellschaft, Berlin-Siemensstadt, Germany, a. corporation of Germany Application December 16,

In Germany December 21,

6 Claims.

j Our invention relates to a system for the concording to our invention at least four heat reservoirs of difierent temperature are in heat exchange relation with those parts of the heat converters, in which an evaporation or a condensation and generation or absorption of an operating medium takes place. The heat converter may consist in this case of only one absorption apparatus or also of various apparatus, in which, if desired, the heat-absorbing or the heat-radiating parts are in heat exchange relation with one another. Also even if only one absorption .ap-

'paratus is used as a heat converter it may be preferable to cause the single vessels of the apparatus to be brought into heat exchange relation with one another.

The heat reservoirs according to the invention may be sources of heat or heat consuming devices. A heat reservoir, from which heat is supplied to the heat converter is denoted hereinafter as a source of heat, whereas a reservoir, to which heat is supplied from the heat converter is designated as a heat consuming device. By the apparatus according to the invention it is possible to attain the various effects either by utilizing them only for the conversion of heat or by bringing them into heat exchange relation with other heat converters. As heat converters according to the invention intermittent or continuous absorption apparatus, steam power plants, steam accumulators,

in general all such systems are employed, in which heat of a given temperature is converted to heat of another temperature or into another form of energy.

In such a system intermittent absorption apparatus may be employed to advantage and preferably those which operate with a solid absorbent which forms a chemical compound with the operating medium. With chemical absorbents it is possible at least within certain limits of concentration to generate and to absorb the operating medium at a constant temperature. It is, therefore, possible to supply to or the single parts of the absorption apparatus at a constant temperature. Since it is essential in manycases to operate within certain constant limits of temperature in the case of heatconverting systems, the use of the above-mentioned substances is very advantageous.

However, on the other hand, the intermittent absorption apparatus have the disadvantage that particular devices, when used in connection with to abstract heat from 1933, Serial, No. 102,810 1932 heat converting systems, are required to reverse the heat transfer devices when changing periods. Such reversing devices may be dispensed with when using absorption apparatus of the continuous type. For this reason such apparatus are preferable in many cases.

In the accompanying drawings some embodiments of our invention are illustrated in diagrammatic form. I

Fig. 1 shows as an embodiment of our invention a system for the conversion of heat, in which two intermittent absorption apparatus are employed.

Fig. 2 shows an embodiment, in which a continuous reabsorption apparatus is employed.

Fig. 3 shows another embodiment in which the heat converter is employed to produce-by applying heat supplied from a reservoir of mean temperature-heat at two higher temperatures and refrigeration at a lower temperature.

Fig. 4 shows a system in which two continuous reabsorption apparatus are employed for the production of refrigeration at a low temperature and for driving two turbines.

Fig. 5 shows a further embodiment in which a heat converter is employed for driving three turbines of different pressure stages and for producing refrigeration at a low temperature.

Fig. 6 is a diagramillustrating .the circulation of the operating medium in the system shown in Fig. 5.

The system shown in Fig. 1 renders it possible to utilize a source of heat of very high temperature in such a manner as to drive a steam turbine, to produce refrigeration and to supply heat of medium temperature. The generator-absorbers of the intermittent absorption apparatus are designated by KA 1, KA. 2 and the corresponding evaporators by CV I, CV 2. The numeral I denotes the source of heat of high temperature (T3). The source of heat may alternately heat either generator-absorber by means of a heat transfer system operating with a circulating medium. The transfer system consists as will be seen from Fig. 1 of a coil 2 contained in the heat generator I, of the coils 3 and 4 disposed in the respective generator-absorbers and of the circulating conduits in which valves 5, 6 are arranged which serve to reverse the circulation in the system. The heat of absorption at a temperature T2 is transferred from the generator-absorber. to the water vapor generator I by means of a circulating system which consists of a coil 8 contained in the vapor generator I and of the coils 9 andlfl contained in the respective generator-absorbers and 0f the corresponding circulation conduits.

Valves I I and I2 which serve to alternately reverse the circulation in the system are also arranged in the circulation conduits.

The heat of absorption is supplied to the water contained in the water vapor generator I and is caused to evaporate therein. The vapor passes through a conduit I3, in which the vapor of the waste gases of the source of heat I may be, if desired, superheated, into a turbine I4 where it expands. A waste steam conduit I5 leads to a condenser I6. Here the vapor is condensed and the heat of condensation liberated during the condensation is utilized for heating purposes in a transfer system I! at the temperature T1. The condensate is again forced into the steam generator I by means of a pump I8.

The condenser-evaporators CV I and CV 2 are provided with heat transfer coils I9 and which appertain to a transfer system, which serves to abstract heat required for the evaporation of the operating medium from a cooling chammr 2| at the temperature To.' To this end, a coil 22 is arranged in the cooling chamber 2 I, the coil 22 being connected as will be seen from Fig. 1 to the coils I9 and 20. 23 and 24 denote two reversing valves arranged in this system.

The heat of condensation liberated during the generating period is utilized for heating purposes. To this end, the transfer coils 25, 26 located in the condenser-evaporators are used which form with a cooler 28 and the corresponding valves 29 and 30 a heat transfer system. The heat of condensation of the operating medium of the ab:- sorption apparatus is transferred from the cooler 28 to a heat transfer system 3 I, where the heat is utilized at the temperature T1 for heating purposes.

In the valve position shown in Fig. 1 the absorption apparatus Kit 2, CV 2 operates during its generating period and the apparatus KA I, CV I during its absorption period. After a certain time has .elapsed all valves are rotated in clockwise direction 90? from the position shown in Fig. 1 so that the absorption apparatus KA 2, CV 2 now operates during its evaporating period and the apparatus KA I, CV I during its generating period. Consequently, the system ensures a continuous production of refrigeration for the cooling chamber 2i, 9, continuous withdrawal of heat forheating purposes in the coils 3i, I! as well as the omration of the turbine 4 owing to the continuous supply of heat to the steam generator I. As compared to the usual absorption refrigeration apparatus (a heat converter with three reservoirs) refrigeration is produced at a somewhat higher temperature and besides additional work is performed in the novel system with four reservoirs with approximately the same quantity of heat.

In the intermittent absorption apparatus strontium bromide may be, for instance, employed as the absorbent and ammonia as the refrigerant (operating medium). Instead of using the condensing apparatus as disclosed in Fig. 1 it may be convenient to employ reabsorption apparatus.

Water may be used in the heat transfer systems for the high temperature and sulphurous acid or ammonia for the'low temperature. These media which serve for the transfer of heat are evaporated in the heat-absorbing parts of the heat transfer systems and condensed in the heatradiating parts thereof.

Fig. 2 shows a system, in which a continuous reabsorption apparatus is employed and in which a high heating temperature I: is utilized for the production of refrigeration atthe temperature To, for driving a turbine between the temperatures T2 and T1 and for supplying heat at the temperature T1. IOI denotes the generator of the intermittent absorption apparatus, to which the heat of generation is supplied at a temperature T3 by means of a heating device I02. The vaporous operating medium passes through a conduit I03 into a reabsorber I04, in which a cooling coil I05 is arranged, by means of which heat is given up at the temperature T1 I06 is'the evaporator of the continuous absorption apparatus, to which heat required for the evaporation of the 1 operating medium is supplied, for instance, from a cooling chamber by means of a coil I01 arranged in an evaporator. The vaporous operating medium passes from the evaporator I06 through a conduit I08 to the absorber I09 where it is reabsorbed by the weak absorption solution; The circulation conduits H0, I I I, H2, and H3 for the absorption solution which are in heat ex-- change with one another are provided, on the one hand, between the generator IM and the absorber I09 and, on the other hand, between the reabsorber I04 and the evaporator I06. The heat exchangers are denoted by WA I and WA 2.

A throttle valve V1 is arranged in the conduit leading from the generator IM to the absorber I09 and a pump P I which serves to cause a circulation of the solution is arranged in the conduit leading from the absorber I09 to the generator IIO. In a corresponding manner a throttle valve V2 is arranged in the conduit H3 and a pump P 2 in the conduit II2. By means of the above-described circulation conduits the absorption solution flows from the generator IOI into the absorber -I09, and after being-enriched with the operating medium flows back into the generator IOI. In the same manner the solution enriched with the operating medium in the reabsorber I04 passes into the evaporator I06, whereas the weak solution is forced back into the reabsorber. The heat of absorption liberated at the temperature T2 serves to evaporate the operating medium of a turbine M1. To this end, a boiler H4, in which water is evaporated for driving the turbine M1 is located in the absorber I09. The vapor passes through a conduit II5leaving the-boiler H4 at the upper part thereof, in which conduit the vapor may, if desired, be superheated by the gaseous products of combustion of the furnace I02into the turbine where it expands. The waste steam flows through a conduit II6 into the condenser I IT. The heat liberated during the condensation is given up to the liquid flowing through a coil I I8, the liquid thus heated serving for heating purposes. The condensate flows through a conduit I I 9 into a feed pump P 3, from which it is conveyed again to the vessel I I 4. A conduit I20 which leads, on the one hand, -to the absorber I09 and, on the other hand, to a discharge conduit in which a valve V19 is arranged is connected to the lower Causticsoda or caustic potash solution or a -mixt11re of both may be employed as the 'absorbent and steam as the. operating medium in the reabsorption apparatus. It is also possible to use different absorbents in the systems IM and I09 and I04, I06; for instance, in the first system zinc chloride and in the second system water. The operating medium is in this case ammonia. The systems are filled through connections provided with valves V5 and V6. If the substances used in the systems are solid at room temperature it is preferable to providethe system I0], I09 with a device which maintains such a temperature that the substances remain liquid not only after a considerable standstill of the system but also when the latter is being filled. To this end, all conduits and vessels may be provided with a steam heating device which is cut ofi dur-- tion solution of different concentration is contained belong to the heat converter. Heat is supplied to the vessels 202 and 203 at the tempera.- ture T1. For this purpose, the coils 201, 208 located in these vessels are employed, through which a heating medium,\for instance, a liquid flows.

These vessels may be heated, if desired, by waste steam or other sources of heat.

Owing to the application of heat, the operating medium'is driven off from the vessel 202 and passes through a conduit 209 into the vessel 20I operating as. reabsorber. The vaporous operating medium is absorbed in the reabsorber 20I. The heat liberated during the absorption is carried off at the temperature To to a heat consumer (not shown)v by means of a medium flowing through the coil 2I0.

The weak solution flows from the lower part of the generator 202 through a conduit 2i I, a pump P 6 and through a heat exchanger WA 4, a conduit 2I2, a second heat exchanger WA 5 and a conduit 2I3 into the upper part of the vessel 205 which operates as ab'wrber. The heat of absorption is carried on from the vessel 203 by means of a coil 2 located therein to a heat consumer (not shown) at the temperature T3.

The vessel 205 operates as a generator. vaporous operating medium driven off at this point passes through a conduit 2I5 into the absorber 206 where it is absorbed by the weak solution flowing thereinto through the conduit 2I3. The solution enriched with the operating medium flows from the absorber 206through a conduit 2 I 0 into the heat exchanger WA 5 and through a conduit 2II provided with a throttling valve V11 into the upper part of the vessel 204. In this vessel a further amount of operating medium is absorbed by the solution flowing into the upper part thereof, so that the concentration of the so lution is further increased. The heat liberated during the absorption is carried off at the temperature T2, i. e., a portion of the heat is carried ofi to a heat consumer (not shown) by the liquid flowing through a coil 2I9, whereas the other portion of heat is supplied to the generator 205 for the purpose of generating theop'erating medium. To this end, a heat transmission system is employed which consists of a coil 220 located in the container 204,

The

of a coil 22I arranged in the vessel 205 and of a conduit 222. In this system a liquid operates in the usual manner, evaporating in the lower portion and condensing in the upper portion. Va-

porous operating medium is supplied through a- 5 conduit 223 from the vessel 203 which operates as a generator to the vessel 2I4 operating as the absorber.

The absorption solution of high concentration flows from the lower part of the absorber 204 into the upper part of the generator 202 through a conduit 224, the heat exchanger WA 4 and through a conduit 225 provided with a valve V12.

Between the vessel 20I, 203, 205 a circuit for the circulation of the solution is provided in the 15 same manner as between the vessels 202, 204 and v 206. From the lower part of the absorber 20I the absorption solution of high concentration forced by a pump P I passes into the upper part of the generator 205through a conduit 226, a heat ex- 20 changer WA 6, a conduit 221, a heat exchanger WA 4 and through a conduit 228. As soon as a portion of the operating medium has been expelled the absorption solution'of a correspondingly lower concentration flows from the lower 25 part of the generator 205 through a conduit 229, I a heat exchanger WA 1, a conduit 230 provided with a valve V13 into the upper part of the generator' 203. There, further operating medium is abstracted from the solution inthe usual man- 3 ner by evaporation and the weak solution flows from the lower part of the generator 203 back into the upper part of the absorber 20I through a conduit 23I, heat exchanger WA 6 and through a conduit 232-provided with a valve V14. The ab- 35 sorber 20I is connected to the generator 202 by a conduit 233, which is provided with a discharge conduit-and the valves V11, V18, V20. The conduits provided with the valves V15, V16 are used for filling" the fluids. 40

The heat converter is, for instance, filled with aqueous caustic soda solution.

The system 20I, 203 may also be designed as a condensation system. In case the vaporous operating medium coming from the vessel 202 through the conduit 209 is condensed in the vessel 20I; the condensate-passes into the vessel 205 through, the pump P I, the conduits 226, 221, the heat exchanger WA I and through the conduit 228. The heat exchanger WA 5 is omitted in this case. A portion of the liquid operating medium is evaporated in vessel 205 by the heat transferred from the vessel 204 and the vaporous operating medium flows into the condenser 205 through the conduit 2| 5. The remaining portion of the operating liq- 55 uid leaves the vessel 205 through the conduit 220, heat exchanger WA I, conduit 230, valve V1: and passes into the vessel 203 where it is evaporated by application of heat.

Under these circumstances it is preferable to insert an equalizing conduit with a valve between the vessels 203 and 20I.

Accordingly, the above-described heat converter may also be employed to supply heat at the temperatures T0, T2 and T3 and to produce heat at the temperature T1. In this case the functions of the single vessels are simply reversed.

The heat liberated in the absorber 20I may be carried off to a heat consumer, for instance, to .river water.

Fig. 4 shows a system, in which two continuous reabsorption apparatus are employed, and in which a high heating temperature T4 is utilized for the production of refrigeration at the temperature To, fordriving a turbine between the temperatures T2, T1 and a second turbine between the temperatures T3, T2 as well as for supplying heat at the temperature T2. I M denotes the generator oi the intermittent absorption apparatus. The heat of generation is, for instance, supplied to the generator at the temperature T4, by means of a heating device I02. The vaporous operating medium passes through a conduit I03 into a reabsorber I04, in which a cooling coil I05 is located. I06 is the evaporator of one of the continuous reabsorption apparatus. The heat required. for expelling the operating medium is supplied to the evaporator I06 by means of a coil. I01 arranged therein. The vaporous operatingmedium passes from the evaporator I06 into the absorber I09 through a conduit I08 and is again taken up in the reabsorber I09 by the weak absorption solution. The conduits IIO, III, H2, H3 for the circulation of the absorption solution which are in point III.

heat exchange relation with one another are pro vided between the generator IOI and the absorber I09, one the one hand, and the reabsorber I04 and the evaporator I06, on the other hand. These heat exchangers are designated in Fig. 4 by WA. In the conduit leading from the generator IN to the absorber I09 a valve V1 is inserted and in the conduit I I0 leading from the absorber to the generator a pump P I is provided for circulating the solution. In a corresponding manner a valve-V2 is arranged in the conduit H3 and a pump P 2 in the conduit II2. By means of the above-described circuits theweak absorption solution passes from the generator I 0! to the absorber I09, from which it flows after being enriched with the operating medium back into the generator IOI.

-In the same manner the solution enriched with the operating medium in the reabsorber I04 passes into the evaporator I06, whereas the weak solution after evaporating flows back into the reabsorber I04. The heat of condensation liberated at the temperature Ta serves to heat the operating medium of a turbine M1. To this end, a boiler H4, in which the liquid operating medium serving to drive the pump is evaporated, is arranged in the absorber I09: The vapor passes into the turbine M1 where it expands through a conduit II-5 connected to the upper part oi the boiler I I4.

The waste steam passes through a conduit IIB into the condenser H1. The heat liberated during the condensation is given up to the liquid flowing through a coil I I8 and which is employed for heating purposes. The condensate flows through a conduit I I 9 into aieed pump P 3, from which it is again conveyed to the vessel I04. The conduit I03 leaving the generator IOI and-conveying the vaporous refrigerant branches oil at A portion 01' the vaporous refrigerant is reabsorbed in the reabsorber I04 at the temperature T2, whereas the other portion passes through a conduit I22 into the condenser I23 where the heat of reabsorption is carried oil at the temperature T1 by means oi thecooling coil I24 arranged therein.

The liquid operating medium flows through a conduit I26, a valve V30 into the evaporator I26. to which the heat required for the evaporation of the refrigerant is supplied, for instance. from a. cooling chamber. (not shown) at the temperature To by means of a coil I21 arranged in the evaporator I28. The vaporous operating medium passes from the evaporator I26 through a conduit I28 into a reabsorber I29 where it is absorbed by the weak absorption solution contained therein. The heat liberated during the absorp-- oration oi' the operating medium, cooperates with 5 the reabsorber I29. The absorption solution circulates between the vessels I29 and I2I through conduits I33, I34. A pump P 5 is provided in the conduit I33 to cause a circulation of the absorption solution and a valve V31 is provided in the conduit I34 to regulate the circulation. The said circulation conduits are arranged at the central portion thereof to provide a heat exchanger WA 3. The operating medium expelled from the evaporator I3I passes through a. conduit I33 and 15 the conduit I08 to the point I38 where it combines with the operating medium expelled from manner into the condenser I I1, whereas the other portion is supplied to a turbine M2 through a conduit I 33. The operating medium (steam) ex- 25 panded in the turbine M2 is finally supplied to a condenser I40 through a conduit I39 and con' densed therein. a

The heat liberated during the condensation is carried off by means of a heat transfer system 30 consisting of a coil I4I contained in the condenser I40, of the conduit I42 and of the coil I01 contained in the evaporator I06. In this manner, the heat of condensation of the waste steam of the turbine M2 is employed for evaporating the oper- 35 ating medium in the evaporator I 06. The liquid operating medium in [the turbine is conveyed from the condenser I40 by means of a pump P 4 and a conduit I 43 to point I44 where it combines with the condensate coming irom the condenser 40 I I1 through the conduit H9 and is forced back together .with the condensate into the vessel II4 through the pump P 3. At the lower part of the evaporator I06 a conduit is connected to the valves V3, V4 V1 and V19 which serves the same 45 purposes as described in Fig. 1. A further equalizing conduit I43 with a valve V10 is arranged between the vessels I26 and I3I.

In the system l0I, I09 liquid zinc chloride may be employed as the absorption medium, whereas 50 in the other system water, ammonia being used as the operating medium. According to the invention .the system I23, i20 may also be designed as reabsorption system. In this case the vessel I23 is designed as reabsorber and the 55 connectionof both" vessels I23 and H6 is designed in a manner corresponding to the connection between the vessels I29, I3I.

thereby expelled passes through aconduit 303 to a branch 'point 304. At this point a portion of the vapors passes through a conduit 305 into a 1 reabsorber 300, whereas the other portion passes through a conduit 301 into a condenser 308.

The operating medium is condensed in the con- 15 denser by means of a coil arranged therein which carries off the heat of condensation at the temperature T1. The condensate flows into the evaporator 3| I through a conduit 310, in which a throttle valve V2 is arranged. A coil 3l2 through which the heat required for the evaporation is supplied, for instance, from a cooling chamber is located in the evaporator 3. The vaporous refrigerant passes into the absorber 316 through a conduit 3l3, a point 3 and through a conduit The reabsorber 306 is in heat-exchange relation with an evaporator 3" as will be seen from Fig. 5 through a heat circulating system for the absorption solution and a heat exchanger WA 8. A pump P l2 serves to circulate the solution and-a valve V21 to regulate the same.

A similar circulating system for the absorption liquid with a heat exchanger WA 9 is arranged between the generator 30! and the absorber 316. In this case a pump P H serves to circulate the liquid and a valve V23 to control the circulation of the same.

The heat liberated in the absorber 3l6 at the temperature T4 and in the reabsorber 306 at the temperature T3 is utilized to evaporate an operating medium for three turbines M3, M4, M5. To this end, a steam boiler 3l8 is arranged in the absorber 3I6 and a steam boiler 3!!! in the reabsorber 306. The steam produced in'these boilers may be superheated by the gaseous products of combustion of the furnace 302. The steam passes from the steam boiler 3i0 through a conduit 320 into a turbine M3, whence it passes through a waste steam conduit 32l to a point 322 where it combines with the steam supplied through a conduit 323 and generated in the steam boiler 3l9. From this point, the steam flows through a conduit 324 into the turbine M4 of the medium pressure stage, whence the waste steam is transferred to a branch point 326 through a conduit 325. A portion of the waste steam flows through a conduit 32! into a condenser 328, whereas the other portion passes through a conduit 329 into the turbine M; of the lowest pressure stage. The waste steam passes from the turbine M5 through a conduit 330 into a condenser 33l where it is condensed at the temperature T1 by means of the water cooling coil 332. The condensate is forced by a pump Pa through a conduit 333 to the point 334, where it combines with the condensate coming from the 328 of a condenser coil 340 contained in the evaporator 3 l I and of the conduit 3 and. operating with aliquid which alternately evaporates and condensates, operates between the condenser 328 for the waste steam coming from the turbine M4, on the one hand, and the evaporator 3H, on the other hand. In this manner the heat of condensation is supplied at the temperature T: to the evaporator 3ll.

The vessels 3H, 3", 316 are connected by a conduit which is provided with the stop valves V24, V25, V25, V21. This conduit may be employed, for instance, for evacuating the systems. To fill the systems the vesels 30l and 306 are provided 'converter and thermal power engines as disclosed in the system of Fig. 5 is again shown in diagrammatic form in Fig. 6. Such a plant may be employed either to attain an increased production of refrigeration with a decreased production of power or to attain an increased production of power with a decreased production of refrigeration. Whether more power or refrigeration will be produced depends upon how the vaporous operating medium leaving the generator 30l is distributed over the vessels 306 and 308.

If, for instance, all vaporous operating medium generated in the generator MI is taken up in the vessel 306 no vaporous operating medium is left for the system which produces refrigeration. In this case no refrigeration will, consequently, be produced.

However, since the quantity of vaporous operating medium supplied to the vessel 306 is very great, the quantity of steam which is available for producing the steam necessary to drive the turbine M4 is also very great. On the other hand, a corresponding great quantity of the operating medium must be evaporated in the vessel 3, which implies that a great quantity of heat is also abstracted from the vessel 328.

In this manner the steam produced in excess in the vessel 3!!! and utilized in the turbine M4 is condensed in the vessel 328. With decreasing production of refrigeration the power developed by the turbine M4 is, consequently, increased and reversely.

If an increased production of refrigeration is to be attained with decreased demand of power all the steam flowing through the turbine M3 may be, for instance, condensed in the vessel 3l9. In

this case the vessel 306 of the heat converter acts as a generator. Accordingly, the vessel 3" of the heat converter must, therefore, operate as anabsorber. The heat of absorption is then used to produce steam which is utilized in the turbine M5. In this case the turbine M4 does not perform any work. All intermediate stages may, Of course, be also adjustable.

If a heat consuming means is available at the temperature To which may, for instance, consist in the form of stored cold or in cold as available in nature the operation of the vessels 308 and 3 may be also reversed. In this case the vessel 3 acts as a condenser and the vessel 308 as an evaporator.- The heat liberated in the condenser 331 may then be utilized to evaporate the operating medium in the vessel 308.

The dotted and solid arrows in Fig. 6 are to indicate the quantity of operating medium circulating in the heat converter and in the thermal power plant. The solid arrows indicate a case in which the production of refrigeration is increased and the production of power decreased, whereas the dotted arrows indicate a case of decreased production of refrigeration and an increased production of power. The arrows provided with a circle illustrate aform of operation in which the vessel 3| I gives up heat, for instance, to a heat reservoir availablein nature exchange relation it is possible as the above em-- bodiments show to produce various thermal effects and to perform work at the same time. It is, for instance, possible to supply heat at a very high temperature and to prevent the thermal power engines from coming into contact with this higher temperature. Moreover, a reservoir of low temperature available in nature may be utilized to produce power without it being necessary to cause the medium operating in the thermal power engine to reach these low temperatures. It is, therefore, possible to utilize great differences of temperature in a reversible and easy manner for the production of thermal power without departing from the usual design of the power plants.

Furthermore, it is also possible to produce refrigeration and to perform work as well as to give up heat, if desired, by the above described means.

We claim as our invention:

1. In a system for the conversion of heat in which at least four quantities of heat are totally supplied or carried ofi at different temperatures. a heat converter closed against the outside and operating as an absorption apparatus, said heat converter comprising at least four main parts, i. e., at least two operating vapor developing parts and two parts in which operating vapor is converted into another state of aggregation, at least four outer heat reservoirs in which different temperatures prevail, said heat reservoirs comprising heat sources and heat consuming devices, and heat exchange means between said main parts of the heat converter, on the one hand, and said heat reservoirs, on the other hand, at least one of said heat consuming devices serving to supply heat to a'system combined with said heat converter.

2. In a system for the conversion of heat in which at least four quantities of heat are totally supplied or carried off at diflerent temperatures, a heat converter closed against the outside and operating as an absorption apparatus said heat converter comprising at least four main parts, i. e., at least two operating vapor developing parts and two parts in which operating vapor is converted into another state of aggregation, at least four outer heat reservoirs in which different temperatures prevail, said heat reservoirs comprising heat sources and heat consuming devices. and heat exchange means between said main parts of the heat converter, on the one hand, and said heat reservoirs, on the other hand, 'at least two heating systems being combined with said heat converter, at least two of said heat consuming devices comprising heating means serving to operate said heating systems.

3. In a system for theconversion of heat in which at least four quantities of heat are totally supplied or carried ed at diflerent temperatures,

a heat converter closed against the outside and operating as an absorption apparatus, said heat converter comprising at least four main parts, i. e., at least two operating vapor developing parts and two parts in which operating vapor is converted into another state of aggregation, at least four outer heat reservoirs in which different tema continuously operating absorption apparatus comprising at least four main parts, i. e., at least two operating vapor developing parts and two parts in which operating vapor is converted into another state of aggregation, at least four outer heat reservoirs in which different temperatures A prevail, said heat reservoirs comprising heat sources and heat consuming devices, and heat exchange means between said main parts of the heat converter, on the one hand, and said heat reservoirs, on the other hand, at least one of said heat consuming devices serving to supply heat to a system combined with said heat converter.

5. In a system for the conversion of heat in which four quantities of heat are totally supplied r.

or carried off at different temperatures, a heat converter comprising a plurality of absorption apparatus closed against the outside and each having at least four main parts, i. e., at least two operating vapor developing parts and two parts in which operating vapor is converted into another state of aggregation, at least four outer heat reservoirs in which different temperatures prevail, said heat-reservoirs comprising heat sources and heat consuming devices, and heat exchange means between said main parts of the .heat converter, on the one hand, and said heat reservoirs, on the other hand, at least one of said heat consuming devices serving to supply heat to a system combined with said heat converter.

6. In a system for the conversion of heat in which four quantities of heat are totally supplied or carried off at diirerent temperatures, a heat converter comprising a plurality of absorption apparatus closed against the outside and each having at least four main parts, i. e., at least two operating vapor developing parts and two parts in which operating vapor is converted into another state of aggregation, at least four outer heat reservoirs in which different temperatures prevail, said heat reservoirs comprising heat sources and heat consuming devices, and heat exchange means between said main parts of the heat converter, on the one hand, and said heat reservoirs, on the other hand, at least one of said heat consuming devices serving to supply heat to a system combined with said heat, converter. and heat exchange means between one of said main parts of one of said absorption apparatus and a main part of a second absorption apparatus.

KURT V. NESSELMANN. EDMUND AL'I'ENKIRCH. 

